US3770616A - Method of reforming hydrocarbons - Google Patents

Method of reforming hydrocarbons Download PDF

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Publication number
US3770616A
US3770616A US00140594A US3770616DA US3770616A US 3770616 A US3770616 A US 3770616A US 00140594 A US00140594 A US 00140594A US 3770616D A US3770616D A US 3770616DA US 3770616 A US3770616 A US 3770616A
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Prior art keywords
catalyst
percent
weight
platinum
reaction
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Expired - Lifetime
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US00140594A
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English (en)
Inventor
N Kominami
T Iwaisako
K Ohki
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Asahi Kasei Corp
Asahi Chemical Industry Co Ltd
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Asahi Chemical Industry Co Ltd
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Priority claimed from JP45040914A external-priority patent/JPS4941181B1/ja
Priority claimed from JP46005972A external-priority patent/JPS5228781B1/ja
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/63—Platinum group metals with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
    • B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
    • B01J23/628—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with lead
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/66—Silver or gold
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8966—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with germanium, tin or lead
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/085—Catalytic reforming characterised by the catalyst used containing platinum group metals or compounds thereof
    • C10G35/09—Bimetallic catalysts in which at least one of the metals is a platinum group metal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Definitions

  • ABSTRACT Method of reforming hydrocarbons which comprises treating a mixture of hydrogen and hydrocarbon at a temperature from 400C. to 650C.
  • a catalyst containing from 0.01 to 5 percent by weight of platinum, from 0.01 to 5 percent by weighth of lead and from 0.01 to 10 percent by weight of at least one member selected from the group consisting of copper, silver, gold, boron, thallium, titanium, zirconium, vanadium, tantalum, manganese, iron, cobalt, nickel, thorium, yttrium, phosphorus, antimony, cerium, scandium, gallium, indium, hafnium and niobium.
  • This invention relates to a methodof reforming hydrocarbons and catalyst used therefor. More particularly, it is concerned with a method of reforming hydrocarbons using a catalyst containing platinum, lead and a third component which is used for reforming reaction mainly involving dehydrogenation of naphthenes and isomerization and dehydrocyclization of paraffins.
  • the prior-art platinum-alumina catalyst which is low in activity and high rate of deactivation, was hardly used under severe reaction conditions. For example, the use in the operation at a low pressure such as about 10 kg./cm. or in the operation at a high space velocity (SV) was not economical.
  • SV space velocity
  • This invention relates to catalytic composition containing, in addition to platinum and lead, a third promoter component and a method'of reforming hydrocarbons using the same.
  • the third component are used copper, silver, gold, boron, thallium, titanium, zirconium, vanadium, tantalum, manganese, iron, cobalt, nickel, thorium, yttrium, phosphorous, antimony, cerium, scandium, gallium, indium, hafnium and niobium.
  • the starting material for the platinum, lead and third components may be used a metal or a compound such as oxide, hydroxide, hydrate, salt with an organic or inorganic acid or the like. Particularly with the platinum, it is preferred to use a halogen-containing compound thereof thus preparing a halogen-containing catalyst.
  • the amount of the components added may be optionally chosen depending upon the conditions under which the catalyst is prepared or used.
  • the catalyst contains 0.01-5percent by weight, especially 0. l-lpercent by weight of platinum, 0.01-5 percent by weight, especially 0.l-2 percent by weight of lead and 0.0l percent by weight, especially 0.05-2 percent by weight of the third component.
  • the ratio of platinum to lead of more'than l to 3, namely, the amount of lead contained by less than 3 times the amount of platinum produces more effective catalysts. The reason why the ratio of platinum to lead is defined in such a manner is considered to be in the action of lead as poisonous to platinum when contained beyond such a range as defined above.
  • the carrier may preferably be used silica, silicaalumina, alumina or the like.
  • Alumina produces especially good results.
  • the reforming reaction as referred to herein which is carried out using the above-mentioned catalyst, means dehydrogenation of naphthenes, isomerization, hydrocracking and dehydrocyclization of paraffins and the like.
  • hydrocarbon are commercially'conveniently used naphtha, kerosene, gas oil and the like, although a purehydrocarbon may be used.
  • the hydrogencontaining gas employed may contain inert gas or gas such as methane, ethane and propane and the like.
  • Byproduct gas in the production of ethylene and the off gas from the instant reaction may be used.
  • the reaction temperature is from 400 to 650C., preferably from 450 to 550C.
  • a pressure from I to 50 kg./cm is applied in the reaction and commercially advantageous is a pressure within the range from 5 to 30 kg./cm.
  • the catalyst of this invention which, when used at a high space velocity under a pressure from 5 to 15 kg./cm affords high yield of aromatics, high octane value as well as low rate of deactivation, is very much economical.
  • the volume ratio of hydrogen to hydrocarbon supplied which has an effect upon the life of the catalyst and/or the composition of the product, is suitably from 1 to 15, preferably from 3 to 10.
  • the rate of feeding which depends upon the reaction pressure and the composition of the product is from 0.1 to 10 hr. in LHSV, preferably from 0.5 to 5.0 hr..
  • EXAMPLE 1 Gamma-alumina was impreganted with an aqueous solution of a mixture of chloroplatinic acid H,[PtCl,]-6H,O, lead nitrate Pb(NO and copper nitrate Cu(NO -3l-I,O, and then subjected to evapora tion to dryness. The resulting mass was calcined at 580C. for 1 hour to prepare a catalyst of the composition (0.5% Pt 0.4% Pb 0.2% Cu)/Al,0 A SUS' 32 reaction tube, 14 mm. in inner diameter, was filled with 10 ml. of the catalyst which was then subjected to reduction under hydrogen at 530C. for 1 hour.
  • a gaseous mixture of hydrogen and naphtha of the composition cited below) of a ratio of 1175 was passed through the reaction tube at an LHSV of 2.0 hr., a reaction pressure of 14 kg./cm. and a reaction temperature of 515C.
  • the yield of the product by weight on the basis of naphtha was given below.
  • the results of the reaction are those on average during 50 hours.
  • Liquid yield 83 Benzene l. Toluene 8.
  • QA (Aromatics containing 8 carbon atoms) 22.
  • CA (Aromatics containing 9 carbon atoms) 9.
  • C -P (Aromatics containing can N N O HF 10 or more carbon atoms)
  • Total aromatics 6 ratio of H to naphtha (identical with one in Example 1) of 1:5.0. Properties of the liquid products were as follows:
  • Catalytic components (Note) 1n Examples 3 and 8. the third component was added to the platinum-alumina catalyst calcined in advance. In other examples, alumine was impregnated with a solution of mixture of the three or four components.
  • EXAMPLE 14 An aqueous solution of chloroplatinic acid l-l [PtCl l- 61-1 0 and lead nitrate Pb(NO,,), respectively V at a concentration of 0.1 mole/liter. was poured onto alumina sol (assay 10 percent by weight), followed by evaporation to dryness. The resulting mass was calcined at 600C. for 30 min. and then impregnated with an aqueous cobalt solution. Evaporation to dryness and calcining at 550C. for 1 hour yielded a catalyst of the composition (0.5% Pt- 0.2% Pb 0.1 Co)/Al O Using 25in].
  • a reaction was carried out for a gaseous mixture of a hydrogen: naphtha (of the composition cited below, which was the same in the examples given hereinbelow) of ratio of 1:5.0 under the conditions: Reaction temperature 510C., Wl-lSV 2.5 hr. and reaction pressure 10 kg./cm.
  • Liquid hydrocarbon yield and yield of aromatics on average during hours on the weight basis of the supplied naphtha were 85.3 percent and 63.2 percent respectively.
  • REFERENCE EXAMPLE 3 REFERENCE EXAMPLE 4 A reaction was carried out under the same conditions as in Example 23 except for composition of the catalyst being (0.3% l t;0.3% Pb)[Al O Research gctan e numbers on average during 50, and 168 hours from -tlEilapsiam'nays 103 2. tes w We claim:
  • a method of reforming a naphtha to increase its aromatics content which comprises contacting a gaseous mixture containing hydrogen and naphtha hydrocarbons wherein the volume ratio of hydrogen to hydro-carbon is in the range l-l5 at a temperature in the range from about 400C. to about 650C. and at a pressure in the range 1-50 kg/cm abs.
  • a hydrogen reduced catalyst consisting essentially of from about 0.01 to about 5 percent by weight platinum, from about 0.01 to about 5 percent by weight lead and from about 0.01 to about 10 percent by weight of an element selected from the group consisting of copper, silver, gold, boron, vanadium, thorium, yttrium and scandium on a carrier therefor selected from the group consisting of alumina, silica, silica-alumina and zeolite, the amount of lead in said catalyst being less than three times that of platinum and the contacting operation being carried out a an LHSV in the range 0.1-10 HR.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
US00140594A 1970-05-15 1971-05-05 Method of reforming hydrocarbons Expired - Lifetime US3770616A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP45040914A JPS4941181B1 (OSRAM) 1970-05-15 1970-05-15
JP46005972A JPS5228781B1 (OSRAM) 1971-02-13 1971-02-13

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FR (1) FR2090058B1 (OSRAM)
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NL (1) NL169963C (OSRAM)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3875048A (en) * 1971-07-05 1975-04-01 Asahi Chemical Ind Reforming process using platinum-lead-third component catalyst and catalyst therefor
US3892657A (en) * 1972-07-17 1975-07-01 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US3909393A (en) * 1972-08-16 1975-09-30 Catalyse Soc Prod Francais Trimetallic reforming catalyst and use thereof
US3915845A (en) * 1973-12-06 1975-10-28 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US3926781A (en) * 1973-10-09 1975-12-16 Shell Oil Co Catalytic cracking of paraffinic naphtha
US3933622A (en) * 1973-12-04 1976-01-20 Exxon Research And Engineering Company Trimetallic hydrocarbon conversion catalyst
US3943050A (en) * 1973-07-26 1976-03-09 Bertolacini Ralph J Serial reforming with zirconium-promoted catalysts
US3986984A (en) * 1975-07-21 1976-10-19 Uop Inc. Method of catalyst manufacture
US4018668A (en) * 1975-01-16 1977-04-19 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic sulfur-free catalytic composite
US4024052A (en) * 1975-11-20 1977-05-17 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4056575A (en) * 1975-06-05 1977-11-01 The British Petroleum Company Limited Chemical process making aromatic hydrocarbons over gallium catalyst
US4071437A (en) * 1974-04-08 1978-01-31 Compagnie Francaise De Raffinage Catalysts for the hydrotreatment of hydrocarbons and a process for the preparation and utilization thereof
US4148833A (en) * 1977-01-12 1979-04-10 Uop Inc. Dehydrogenation using nonacidic multimetallic catalyst
US4157356A (en) * 1976-12-20 1979-06-05 The British Petroleum Company Limited Process for aromatizing C3 -C8 hydrocarbon feedstocks using a gallium containing catalyst supported on certain silicas
US5433841A (en) * 1993-04-12 1995-07-18 Kabushiki Kaisha Nippankenkyusho Method for reforming hydrocarbons
US5435984A (en) * 1992-04-28 1995-07-25 Degussa Corporation Catalyst for the synthesis of chlorine dioxide
US5571763A (en) * 1992-06-02 1996-11-05 Mazda Motor Corporation Exhaust gas purification system and catalyst therefor
US6541417B2 (en) * 1998-05-07 2003-04-01 Institute Francais Du Petrole Catalyst based on a noble group VIII metal containing silicon and possibly boron, and its use in hydrotreating hydrocarbon-containing feeds
US20060140831A1 (en) * 2004-12-28 2006-06-29 Southward Barry W Boron-alumina catalyst support

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2436627A1 (fr) * 1978-09-21 1980-04-18 Catalyse Soc Prod Francais Nouveaux catalyseurs d'hydroreformage catalytique ou de production d'hydrocarbures aromatiques

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2378209A (en) * 1942-11-17 1945-06-12 Shell Dev Process for the production of aromatic hydrocarbons
US2500146A (en) * 1946-07-08 1950-03-14 Union Oil Co Catalysts for conversion of hydrocarbons
US3002920A (en) * 1958-12-10 1961-10-03 Exxon Research Engineering Co Hydroforming catalyst and process
BE745703A (fr) * 1969-02-14 1970-08-10 Raffinage Cie Francaise Nouveaux catalyseurs d'hydroreforming et leur procede d'obtention
BE751079A (fr) * 1969-05-28 1970-11-30 Phillips Petroleum Co Procede de deshydrogenation catalytique
US3630961A (en) * 1969-08-22 1971-12-28 Universal Oil Prod Co Hydrocarbon isomerization process
US3670044A (en) * 1969-07-18 1972-06-13 Phillips Petroleum Co Catalytic dehydrogenation process

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2378209A (en) * 1942-11-17 1945-06-12 Shell Dev Process for the production of aromatic hydrocarbons
US2500146A (en) * 1946-07-08 1950-03-14 Union Oil Co Catalysts for conversion of hydrocarbons
US3002920A (en) * 1958-12-10 1961-10-03 Exxon Research Engineering Co Hydroforming catalyst and process
BE745703A (fr) * 1969-02-14 1970-08-10 Raffinage Cie Francaise Nouveaux catalyseurs d'hydroreforming et leur procede d'obtention
US3700588A (en) * 1969-02-14 1972-10-24 Raffinage Cie Francaise Novel hydroreforming catalysts and a method for preparing the same
BE751079A (fr) * 1969-05-28 1970-11-30 Phillips Petroleum Co Procede de deshydrogenation catalytique
US3670044A (en) * 1969-07-18 1972-06-13 Phillips Petroleum Co Catalytic dehydrogenation process
US3630961A (en) * 1969-08-22 1971-12-28 Universal Oil Prod Co Hydrocarbon isomerization process

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3875048A (en) * 1971-07-05 1975-04-01 Asahi Chemical Ind Reforming process using platinum-lead-third component catalyst and catalyst therefor
US3892657A (en) * 1972-07-17 1975-07-01 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US3909393A (en) * 1972-08-16 1975-09-30 Catalyse Soc Prod Francais Trimetallic reforming catalyst and use thereof
US3943050A (en) * 1973-07-26 1976-03-09 Bertolacini Ralph J Serial reforming with zirconium-promoted catalysts
US3926781A (en) * 1973-10-09 1975-12-16 Shell Oil Co Catalytic cracking of paraffinic naphtha
US3933622A (en) * 1973-12-04 1976-01-20 Exxon Research And Engineering Company Trimetallic hydrocarbon conversion catalyst
US3915845A (en) * 1973-12-06 1975-10-28 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
US4071437A (en) * 1974-04-08 1978-01-31 Compagnie Francaise De Raffinage Catalysts for the hydrotreatment of hydrocarbons and a process for the preparation and utilization thereof
US4018668A (en) * 1975-01-16 1977-04-19 Universal Oil Products Company Hydrocarbon conversion with an acidic multimetallic sulfur-free catalytic composite
US4056575A (en) * 1975-06-05 1977-11-01 The British Petroleum Company Limited Chemical process making aromatic hydrocarbons over gallium catalyst
US3986984A (en) * 1975-07-21 1976-10-19 Uop Inc. Method of catalyst manufacture
US4024052A (en) * 1975-11-20 1977-05-17 Uop Inc. Hydrocarbon conversion with an acidic multimetallic catalytic composite
US4087381A (en) * 1975-11-20 1978-05-02 Uop Inc. Acidic multimetallic catalytic composite
US4157356A (en) * 1976-12-20 1979-06-05 The British Petroleum Company Limited Process for aromatizing C3 -C8 hydrocarbon feedstocks using a gallium containing catalyst supported on certain silicas
US4148833A (en) * 1977-01-12 1979-04-10 Uop Inc. Dehydrogenation using nonacidic multimetallic catalyst
US5435984A (en) * 1992-04-28 1995-07-25 Degussa Corporation Catalyst for the synthesis of chlorine dioxide
US5571763A (en) * 1992-06-02 1996-11-05 Mazda Motor Corporation Exhaust gas purification system and catalyst therefor
US5433841A (en) * 1993-04-12 1995-07-18 Kabushiki Kaisha Nippankenkyusho Method for reforming hydrocarbons
US6541417B2 (en) * 1998-05-07 2003-04-01 Institute Francais Du Petrole Catalyst based on a noble group VIII metal containing silicon and possibly boron, and its use in hydrotreating hydrocarbon-containing feeds
US20060140831A1 (en) * 2004-12-28 2006-06-29 Southward Barry W Boron-alumina catalyst support
US7462338B2 (en) * 2004-12-28 2008-12-09 Umicore Ag & Co. Kg Boron-alumina catalyst support

Also Published As

Publication number Publication date
GB1356400A (en) 1974-06-12
DE2123606A1 (de) 1971-11-25
DE2123606B2 (de) 1977-07-07
NL169963C (nl) 1982-09-16
NL7106670A (OSRAM) 1971-11-17
FR2090058A1 (OSRAM) 1972-01-14
FR2090058B1 (OSRAM) 1974-02-15

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